EP4183864A1 - Procédé et dispositifs pour une séparation solide-liquide partielle ou totale efficace à l'aide de conditions contrôlées par gaz - Google Patents
Procédé et dispositifs pour une séparation solide-liquide partielle ou totale efficace à l'aide de conditions contrôlées par gaz Download PDFInfo
- Publication number
- EP4183864A1 EP4183864A1 EP22208948.4A EP22208948A EP4183864A1 EP 4183864 A1 EP4183864 A1 EP 4183864A1 EP 22208948 A EP22208948 A EP 22208948A EP 4183864 A1 EP4183864 A1 EP 4183864A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- liquid
- gas
- biomass
- solid material
- filtration
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 239000007788 liquid Substances 0.000 title claims abstract description 95
- 238000000034 method Methods 0.000 title claims abstract description 78
- 230000008569 process Effects 0.000 title claims abstract description 52
- 238000000926 separation method Methods 0.000 title description 27
- 230000036961 partial effect Effects 0.000 title description 8
- 239000007789 gas Substances 0.000 claims abstract description 93
- 239000002028 Biomass Substances 0.000 claims abstract description 92
- 238000001914 filtration Methods 0.000 claims abstract description 74
- 238000010438 heat treatment Methods 0.000 claims abstract description 43
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 32
- 239000001301 oxygen Substances 0.000 claims abstract description 32
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 32
- 239000007787 solid Substances 0.000 claims abstract description 30
- 239000011343 solid material Substances 0.000 claims abstract description 26
- 238000012546 transfer Methods 0.000 claims abstract description 16
- 238000011282 treatment Methods 0.000 claims abstract description 14
- 239000000725 suspension Substances 0.000 claims abstract description 12
- 239000013598 vector Substances 0.000 claims abstract description 12
- 230000000717 retained effect Effects 0.000 claims abstract description 10
- 238000006243 chemical reaction Methods 0.000 claims abstract description 9
- 230000016507 interphase Effects 0.000 claims abstract description 8
- 239000000126 substance Substances 0.000 claims abstract description 8
- 230000005587 bubbling Effects 0.000 claims abstract description 5
- 238000011143 downstream manufacturing Methods 0.000 claims abstract description 4
- 239000000203 mixture Substances 0.000 claims description 39
- 241000233866 Fungi Species 0.000 claims description 16
- 239000000706 filtrate Substances 0.000 claims description 9
- 240000004808 Saccharomyces cerevisiae Species 0.000 claims description 5
- 241000700605 Viruses Species 0.000 claims description 2
- 239000000084 colloidal system Substances 0.000 claims description 2
- 238000013386 optimize process Methods 0.000 claims description 2
- 239000000463 material Substances 0.000 description 37
- 238000012545 processing Methods 0.000 description 25
- 230000009467 reduction Effects 0.000 description 23
- 239000006228 supernatant Substances 0.000 description 16
- 238000004519 manufacturing process Methods 0.000 description 14
- 239000000047 product Substances 0.000 description 13
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 12
- 210000004027 cell Anatomy 0.000 description 12
- 230000010412 perfusion Effects 0.000 description 11
- 230000001276 controlling effect Effects 0.000 description 10
- 239000006227 byproduct Substances 0.000 description 9
- 230000015556 catabolic process Effects 0.000 description 6
- 238000006731 degradation reaction Methods 0.000 description 6
- 238000009792 diffusion process Methods 0.000 description 6
- 239000000835 fiber Substances 0.000 description 6
- 229910052757 nitrogen Inorganic materials 0.000 description 6
- 238000011084 recovery Methods 0.000 description 6
- 230000008859 change Effects 0.000 description 5
- 150000001875 compounds Chemical class 0.000 description 5
- 238000010586 diagram Methods 0.000 description 5
- 239000001963 growth medium Substances 0.000 description 5
- 238000001802 infusion Methods 0.000 description 5
- 230000003647 oxidation Effects 0.000 description 5
- 238000007254 oxidation reaction Methods 0.000 description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- 238000000855 fermentation Methods 0.000 description 4
- 230000004151 fermentation Effects 0.000 description 4
- 230000014759 maintenance of location Effects 0.000 description 4
- DLVXCEBZMMWMQK-UHFFFAOYSA-N n-(4-methoxyphenyl)-5-methyl-[1,2,4]triazolo[1,5-a]pyrimidin-7-amine Chemical compound C1=CC(OC)=CC=C1NC1=CC(C)=NC2=NC=NN12 DLVXCEBZMMWMQK-UHFFFAOYSA-N 0.000 description 4
- 102000004169 proteins and genes Human genes 0.000 description 4
- 108090000623 proteins and genes Proteins 0.000 description 4
- 230000003134 recirculating effect Effects 0.000 description 4
- 241000894006 Bacteria Species 0.000 description 3
- 150000001413 amino acids Chemical class 0.000 description 3
- 230000015572 biosynthetic process Effects 0.000 description 3
- 238000009295 crossflow filtration Methods 0.000 description 3
- 238000000605 extraction Methods 0.000 description 3
- 239000012467 final product Substances 0.000 description 3
- 239000012530 fluid Substances 0.000 description 3
- 230000002538 fungal effect Effects 0.000 description 3
- 239000011344 liquid material Substances 0.000 description 3
- 239000000178 monomer Substances 0.000 description 3
- 230000002829 reductive effect Effects 0.000 description 3
- 239000007921 spray Substances 0.000 description 3
- 238000003860 storage Methods 0.000 description 3
- 241000196324 Embryophyta Species 0.000 description 2
- 239000003570 air Substances 0.000 description 2
- 230000003750 conditioning effect Effects 0.000 description 2
- 238000011109 contamination Methods 0.000 description 2
- 238000011217 control strategy Methods 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 230000018109 developmental process Effects 0.000 description 2
- 239000002270 dispersing agent Substances 0.000 description 2
- 239000012510 hollow fiber Substances 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 230000000415 inactivating effect Effects 0.000 description 2
- 230000002779 inactivation Effects 0.000 description 2
- 238000002955 isolation Methods 0.000 description 2
- 239000002609 medium Substances 0.000 description 2
- 244000005700 microbiome Species 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 235000015097 nutrients Nutrition 0.000 description 2
- 229950011087 perflunafene Drugs 0.000 description 2
- UWEYRJFJVCLAGH-IJWZVTFUSA-N perfluorodecalin Chemical compound FC1(F)C(F)(F)C(F)(F)C(F)(F)[C@@]2(F)C(F)(F)C(F)(F)C(F)(F)C(F)(F)[C@@]21F UWEYRJFJVCLAGH-IJWZVTFUSA-N 0.000 description 2
- 229920001296 polysiloxane Polymers 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 239000008247 solid mixture Substances 0.000 description 2
- 235000000346 sugar Nutrition 0.000 description 2
- AZUYLZMQTIKGSC-UHFFFAOYSA-N 1-[6-[4-(5-chloro-6-methyl-1H-indazol-4-yl)-5-methyl-3-(1-methylindazol-5-yl)pyrazol-1-yl]-2-azaspiro[3.3]heptan-2-yl]prop-2-en-1-one Chemical compound ClC=1C(=C2C=NNC2=CC=1C)C=1C(=NN(C=1C)C1CC2(CN(C2)C(C=C)=O)C1)C=1C=C2C=NN(C2=CC=1)C AZUYLZMQTIKGSC-UHFFFAOYSA-N 0.000 description 1
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 241000195493 Cryptophyta Species 0.000 description 1
- 102000004190 Enzymes Human genes 0.000 description 1
- 108090000790 Enzymes Proteins 0.000 description 1
- 241000567178 Fusarium venenatum Species 0.000 description 1
- WQZGKKKJIJFFOK-GASJEMHNSA-N Glucose Natural products OC[C@H]1OC(O)[C@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-GASJEMHNSA-N 0.000 description 1
- 206010021143 Hypoxia Diseases 0.000 description 1
- 241000736262 Microbiota Species 0.000 description 1
- 229920002472 Starch Polymers 0.000 description 1
- 238000010793 Steam injection (oil industry) Methods 0.000 description 1
- CZMRCDWAGMRECN-UGDNZRGBSA-N Sucrose Chemical compound O[C@H]1[C@H](O)[C@@H](CO)O[C@@]1(CO)O[C@@H]1[C@H](O)[C@@H](O)[C@H](O)[C@@H](CO)O1 CZMRCDWAGMRECN-UGDNZRGBSA-N 0.000 description 1
- 229930006000 Sucrose Natural products 0.000 description 1
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 239000011149 active material Substances 0.000 description 1
- 238000013019 agitation Methods 0.000 description 1
- 239000000908 ammonium hydroxide Substances 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 238000011001 backwashing Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- WQZGKKKJIJFFOK-VFUOTHLCSA-N beta-D-glucose Chemical compound OC[C@H]1O[C@@H](O)[C@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-VFUOTHLCSA-N 0.000 description 1
- 230000000975 bioactive effect Effects 0.000 description 1
- 239000012620 biological material Substances 0.000 description 1
- 239000000872 buffer Substances 0.000 description 1
- 239000007853 buffer solution Substances 0.000 description 1
- 239000004202 carbamide Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000004113 cell culture Methods 0.000 description 1
- 239000006285 cell suspension Substances 0.000 description 1
- 230000003833 cell viability Effects 0.000 description 1
- 238000005119 centrifugation Methods 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000001143 conditioned effect Effects 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 239000007857 degradation product Substances 0.000 description 1
- 230000000593 degrading effect Effects 0.000 description 1
- 238000011026 diafiltration Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 229920002313 fluoropolymer Polymers 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 230000008014 freezing Effects 0.000 description 1
- 238000007710 freezing Methods 0.000 description 1
- 239000008103 glucose Substances 0.000 description 1
- 230000007954 hypoxia Effects 0.000 description 1
- 238000012994 industrial processing Methods 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 238000004898 kneading Methods 0.000 description 1
- 230000000670 limiting effect Effects 0.000 description 1
- 150000002632 lipids Chemical class 0.000 description 1
- 239000006194 liquid suspension Substances 0.000 description 1
- 210000004962 mammalian cell Anatomy 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 230000037353 metabolic pathway Effects 0.000 description 1
- 230000004060 metabolic process Effects 0.000 description 1
- 239000002207 metabolite Substances 0.000 description 1
- 238000009740 moulding (composite fabrication) Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 150000002978 peroxides Chemical class 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000003755 preservative agent Substances 0.000 description 1
- 102000004196 processed proteins & peptides Human genes 0.000 description 1
- 108090000765 processed proteins & peptides Proteins 0.000 description 1
- 238000011946 reduction process Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 230000000241 respiratory effect Effects 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 150000003384 small molecules Chemical class 0.000 description 1
- 239000008107 starch Substances 0.000 description 1
- 235000019698 starch Nutrition 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 239000000758 substrate Substances 0.000 description 1
- 239000005720 sucrose Substances 0.000 description 1
- 150000008163 sugars Chemical class 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M47/00—Means for after-treatment of the produced biomass or of the fermentation or metabolic products, e.g. storage of biomass
- C12M47/12—Purification
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M47/00—Means for after-treatment of the produced biomass or of the fermentation or metabolic products, e.g. storage of biomass
- C12M47/10—Separation or concentration of fermentation products
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D19/00—Degasification of liquids
- B01D19/0005—Degasification of liquids with one or more auxiliary substances
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D19/00—Degasification of liquids
- B01D19/0073—Degasification of liquids by a method not covered by groups B01D19/0005 - B01D19/0042
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D37/00—Processes of filtration
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M47/00—Means for after-treatment of the produced biomass or of the fermentation or metabolic products, e.g. storage of biomass
- C12M47/16—Sterilization
Definitions
- the invention refers to the technical field of processes and devices to obtain partial or total separation of a labile solid from a liquid in a production process.
- the invention uses gas-controlled conditions for the production of biomass and its efficient separation from the dispersant liquid.
- the invention is particularly useful in processes to reduce RNA content of a biomass.
- Filtration is the most common process in industrial operations for dispersed solid-liquid separations. Processes for separation of inert materials are well studied and parameterized.
- a key step in biomass production processes is reduction of RNA content in the biomass downstream of the bioreactor and before the preparation of a final manufactured product, especially in the case where the biomass is a fungal biomass (either from a filamentous fungus or yeasts) and other biochemically active products with high RNA content.
- Existing processes are known and well characterized (See, for example, UK Patent Application Nos.GB2557886 and GB2551964 , and International Publication Nos. WO2018/002581 and WO2018/002579 )
- the methods to reduce biomass RNA content involve a two-step process with two heating treatments, one immediately after the other.
- WO2018002579 describes a process in which a first step includes the heating from 40 to 69 °C, and a second step of increasing the temperature by 2 to 20 °C more, after which the biomass is separated from the other components.
- the treatment machinery is arranged to use the hot material from the second step as a heat source to increase the temperature in the inflow of the first step.
- the present invention solves these and other problems in the prior art by providing a process where the dissolved gases concentration is controlled to a desired level using solid-liquid, liquid-liquid or gas-liquid interfaces, ensuring the control of the dissolved gas level in the liquid, and thus controlling the reaction environment while the processes inside the filter system are occurring.
- the use of microwaves as a heating means can also allow heat treatment of the material within the device without the need of using steam or other hot fluid or convective wall transfer.
- the present invention provides a significant improvement to processes and systems used for separation purposes and solves the main issues generally observed in current industrial separation operations.
- the present invention is a filtration method for downstream processing of a suspension containing a labile solid material in a liquid medium that includes controlling the dissolved gas content in the liquid during filtering to optimize process conditions.
- the dissolved gas content can be controlled by a gas-liquid interphase transfer process by bubbling gas with a composition and a rate to provide a desired gas content; a liquid-liquid interphase transfer process using a gas vector substance charged with a concentration of gas to provide a desired gas content; a liquid-solid interphase transfer process by using a gas permeable solid having a concentration and pressure of gas by the circulation of gas or a gas vector substance within a luminal structure to provide a desired gas content; or controlling the dissolved gas content by use of a reaction evolving oxygen or other gas/gases.
- the solid material is removed in a batch operation or a continuous operation.
- the solid material can also be removed in a mixed-type operation.
- the invention can also include concentrating the suspension by filtration, heat-treatment, and removal of at least a part of the liquid filtrate from the filtration.
- removal of the filtrate is followed by heat-treatment and subsequent removal of additional liquid produced by the heat-treatment by further filtration.
- Heat treatment can be accomplished using steam, a heated gas, a heated liquid, or combinations thereof.
- the heat treatment is accomplished by treatment with microwaves.
- the solid material is a biomass
- the heat treatment inactivates the biomass.
- the biomass may be a fungus, for example a yeast or a filamentous fungus; cells of animal origin; cells of plant or algal origin; cells of protist origin; or a virus or part thereof.
- the solid material can also be a mixture of two or more of a fungus, cells of animal origin, cells of plant origin, and cells of algal origin.
- the solid material can be in the form of, for example, a colloid or an emulsified solid or a mixture thereof.
- the invention is focused on the field of processes and devices for processing reactive entities susceptible to environment conditions during filtration processes.
- the reactive entity is a solid material that is suspended in a liquid.
- the solid is a biomass such as a bacteria, a yeast, or a type of fungi produced by fermentation or other process known in the art.
- the fungus is a filamentous fungus.
- the devices and methods of the invention are used for separation operations where diffusive or convective transport allows for a reactive entity to survive the process unchanged or with a desired change, avoiding difficulties arising from steps generally performed in separation equipment.
- the unchanged or changed state refers to the desired condition for the entity in the context of the process.
- the temperature within the device is controlled to a desired level in various ways, being preferred but not limited to the use of microwaves to heat water and material susceptible to microwave heating.
- Use of microwave heating is advantageous in avoiding temperature gradients caused by wall-to-processed-material convection.
- the process of the invention includes production enhancement of the reactive entity, separation, and content transformation to provide a desired composition, wherein the inactivation is accomplished while maintaining stability of the reactive entity. Also, the process provides the production of soluble or dispersive final product from the reactive entity. While systems and methods of the invention may apply to a broad range of reactive entities, the invention is particularly used in the production of biomass, particularly for biomass that is used to produce food products. In particular examples, the biomass is a filamentous fungus and the invention is used for removal of RNA and byproducts from the biomass.
- the present invention refers to a process where dissolved gas concentration is controlled using solid-liquid, liquid-liquid or gas-liquid interfaces, ensuring the control of dissolved gas level in the liquid during manufacture (for example by fermentation), and controlling the reaction environment during filtration processes. Furthermore, the use of microwaves as a heating means allows heat treatment of the material within the device without the need to use steam or any other hot fluid or convective wall transfer.
- Biomass production is generally performed in bioreactors (stirred tanks, airlift, bubble column, staked trays, perfusion) to grow a microorganism aerobically.
- bioreactors stirred tanks, airlift, bubble column, staked trays, perfusion
- the culture conditions are around 28 °C and pH 5.8 with limited control of concentration of carbon, energy source (i.e. glucose, sucrose, starch) and nitrogen source (i.e. ammonium hydroxide, urea, amino acids).
- Bioreactors work by controlling the pH and temperature in order to keep both the growth rate and the composition of the biomass maximized.
- Nutrients are added at a rate compatible with the productivity requirements for the industrial processing, and mechanical conditions are adjusted to ensure the appropriate shear stress to keep a high percentage of viable cells and maintain a proper physical structure for product applications.
- There are a number of configurations able to produce the biomass including, for example, submerged culture (SmF), solid state culture (SSF) and mixed culture strategies (SmF+SSF). Any of these can be followed by a processing step involving RNA reduction.
- SmF submerged culture
- SSF solid state culture
- SmF+SSF mixed culture strategies
- Any of these can be followed by a processing step involving RNA reduction.
- SmF the processing is generally performed with a liquid accompanying the biomass, whereas in the case of SSF it is generally required to add liquid in order to eliminate soluble molecules secreted by the biomass upon heat treatment.
- the present invention can be used for any biomass as it maximizes concentration of supernatant, increases the recovery of biomass and reduces energy costs to obtain the biomass and the by-product
- Figure 1 illustrates a flow chart of an exemplary embodiment of the invention that may be used for the separation of RNA from a biomass.
- the process of Figure 1 is readily modified to provide improved separations in other situations, for example from suspensions containing labile solids other than biomass or for separating different by-products.
- FIG. 1 illustrates a process 100 for isolation of a solid biomass from a liquid suspension.
- a biomass suspension is provided, for example from a fermenter.
- the biomass is then concentrated in step 104 using a filtering device, for example a filter or centrifuge, as described elsewhere herein, to provide predominately a solid concentrated biomass and predominantly a liquid supernatant that contains culture media, including waste products and by-products, and may contain additional suspended biomass.
- the gas composition of the liquid is controlled to provide an environment similar to that used in the fermentation phase. It has surprisingly been found that controlling gas concentration during this stage has a beneficial effect on the yield and purity of the final product.
- the supernatant may go through further processing or treatment, including, for example an additional filtration step 108, as described elsewhere herein.
- the supernatant may also be stored in which case temperature and gas composition may be controlled to avoid oxidation or degradation. Preservatives may also be added to avoid contamination by ambient microbiota.
- the concentrated biomass can undergo further treatment, which may include heat treatment 106 and/or oxygen reduction to inactivate the biomass.
- Heat treatment may utilize the supernatant for heating.
- the supernatant is heated and then recirculated through the concentrated biomass, both inactivating the biomass and providing a means for isolating additional biomass from the supernatant in an additional solid-liquid separation step 110.
- the supernatant is heated to about 50 to 75 °C. In the case of perfusion bioreactors the temperature can be lowered to be more compatible to mammalian cell culture (37 °C).
- any solids suspended in the supernatant may be returned to the main separation device where the presence of the initial biomass acts as an extra filtration substrate improving filtration and the amount of material accumulated in the filtration apparatus.
- the material in the filtering device for example the concentrated biomass and the recycled supernatant, may be heated using microwave energy.
- This additional separation provides a wet inactivated 114 biomass which, for example, may be on a filter device or in the bowl of a centrifuge, which is then removed in step 112 to provide a wet biomass.
- the wet biomass 114 then undergoes further processing to form a final product.
- the additional solid-liquid separation step 110 also results in the isolation of a concentrated biomass extract 116.
- the concentrated biomass 116 extract may undergo further processing such as isolating RNA monomers and oligomers therefrom or recirculation and regeneration to provide new culture media.
- the concentrated biomass extract may also be spray dried to produce a powder.
- the wet biomass 114 can be spray dried for some applications but can also be dried differently, for example by convective or microwave heating using a tunnel drier.
- the solid composition can also be processed to control its physical characteristics. For example, oxygen contact with the solid composition can provide a stringent texture development due to oxidation on the surface of the solid. As steam controls temperature the properties of the biomass can be modified. A liquid buffer allowing removal or retention of particular components at the biomass would render a different biomass composition. Using a particular pH or salt can control the nature and amounts of proteins, amino acids, etc. that will be removed or retained during further processing.
- filtration elements can use various means for separation of solid from liquid, generally referred to here as filtration elements.
- suitable filtration elements include, but are not limited to:
- the filtration systems used for the process can be either stationary as in Nutsche filtration apparatus or moving as in rotary press filters, spin filter or rotary drums.
- Pusher centrifuges, peeler centrifuges, decanter centrifuges, etc. are also useful filtration mechanisms for the concentration of solids such as a biomass.
- biomass concentration utilizes a centrifuge (for example SPC-01 in Fig 2 ) or a filtration device (TFF-101 in Fig. 3 or DSM Filter in Fig. 2 ).
- the level of the control of gas concentration during the solid concentration stage is based on the biochemical activity or stability of the material.
- the composition can be oxygen rich composition, up to 100%, more commonly 20%.
- the oxygen content can be lowered to avoid undesired oxidation, in some cases lowering the concentration of O 2 to 0%.
- the systems and methods of the invention control gas content in the associated liquids during production (e.g., fermentation) and filtering processes. It has been found that controlling the gas composition allows the production/control of particular physical and chemical properties in the material such as producing or avoiding oxidation, precluding the use of aggressive agitation resulting in a lower shear of the product which can lead to undesired textures in the material. Controlling gas composition can also reduce the presence of by-products and prevent changes in metabolism
- the separation of labile solids from a liquid in which it is suspended is affected by the CO 2 built up and O 2 reduction in the filtering device and the change in temperature which can impact cell productivity.
- the control of the gas composition and temperature within the filtering devices with gas phase or gas vector control strategies as those developed in this invention improves the performance of perfusion cultures outperforming currently available perfusion by reducing CO 2 build up and increasing O 2 concentrations.
- the media acting as gas vectors can be adjusted in order to work in a range of conditions from the saturation to the total exhaustion of that gas component.
- the RNA reduction process is generally a temperature-controlled process, where the internal RNAses (endogenous RNA degrading enzymes) digest the RNA to its monomers reducing the RNA content within a biomass such as a fungus (particularly the mycelium of a filamentous fungus), bacteria, algae, etc.
- a biomass such as a fungus (particularly the mycelium of a filamentous fungus), bacteria, algae, etc.
- the process also results in increasing concentration of monomers and oligomers in the supernatant liquid.
- the concentrated biomass extract is processed to provide a concentration of dissolved solids of more than 20% in order to allow cost-effective recovery of the dissolved material as dried solids using i.e. a spray dryer. Energy expenditure resulting from the treatment of excess liquid, and water evaporation is radically changed when liquid mass in contact with the RNA containing material is reduced using an appropriate filtering device.
- Example 1a Application in RNA reduction using a centrifugal filtration device
- a modified device consisting of a peeler syphon centrifuge with gas and temperature control
- the equipment allows partial dewatering in the peeler syphon centrifuge (SPC-01), supernatant recirculation, heat treatment and final dewatering of the biomass.
- the gas composition and temperature in the SPC-01 is controlled to ensure the conditions to enhance productivity and accomplish RNA reduction and final water content of the biomass.
- the bioreactor liquid stream is introduced into the filtration device (SPC-01) and the free liquid is partially removed to obtain a concentrated biomass with controlled oxygen level, allowing aerobic conditions.
- the material is heated to reach the RNA degradation temperature, for example a temperature from about 50 to about 70 °C, inactivating the biomass.
- the concentrated broth reaches the degradation temperature, the liquid is recirculated in the filtration system to ensure proper extraction of soluble matter and once the soluble concentration remains unchanged or reaches the desired composition, the liquid is separated and the solid removed from the filtration system.
- the heating process is produced by a microwave system ensuring the whole mass heating without fully depending on convective heat transfer as in other systems.
- the biomass suspended in the culture medium enters the SPC-01 (syphon peeler centrifuge) and liquid material is transferred to tank TK-107 for filtration and recirculation.
- the filtration allows the small size biomass recovery by filtration with the TFF-102 filter, recirculating the biomass to the SPC-01 and allowing the better recovery once a bed of material is formed within the centrifuge basket.
- the recirculation involves the passage through a heat exchanger THE-01 to adjust the temperature of the recirculating liquid to ensure proper temperature during heat treatment of the biomass retained at SPC-01.
- the filtrated supernatant during the first phase of operation is directed to storage tanks for subsequent processing, whereas after the first phase of liquid reduction, the liquid is recirculated for temperature and composition control and RNA derived compound extraction.
- the operation may thus include the following steps:
- the use of the proposed device reduces the need of several devices for RNA reduction and increases the efficiency by eliminating the need for second heat treatment.
- This process can be performed with a syphon shaft peeler centrifuge in batch operation requiring approximately 30 min per batch.
- Example 1b Application in RNA reduction using a tangential filtration device
- FIG. 3 shows the equipment for processing cell suspensions using a tangential filtration device with gas diffusion component for oxygen control within the filter.
- the equipment allows partial liquid removal or culture processing within a filtration device (TFF-101) where temperature, gas composition and filtration/perfusion are controlled.
- Cells or the biomass can be either recirculated to the production tank or directed to a storage tank (not shown).
- the filtrate can be either stored in TK-107 or filtered through TFF-102 to perform a particular separation or concentration or just recirculation to ensure fouling reduction in the membrane of TFF-101 by back wash.
- the gas composition and temperature in the TFF-101 is controlled to ensure the conditions to enhance productivity and accomplish the desired process, for example, for the product modification or maintaining cell viability.
- TMFCs Thermal mass flow controllers
- gas composition within the filter is attained by interface contact.
- this interface can be kept controlled by liquid substances containing the gas components (i.e. oxygen vectors for oxygen).
- Filtration through the TFF-102 can be avoided and liquid stream directed for backwashing the TFF-101.
- Temperature control can be enhanced by recirculation using heat exchanger THE-01, to ensure direct contact of temperature conditioned liquid with the filter surface.
- gas-liquid transfer for example, nitrogen, oxygen, or air infusion directly into the liquid
- bubbling gas can be used for gas infusion/diffusion control, particularly during the filtration process.
- gas flow rate can be adjusted due to different factors, particularly due to the bubble size.
- gas flow rate can be 0.1 - 2 VVM (volume of gas relative to volume of the liquid medium per minute) when the bubble size is 3 mm.
- the biomass suspended in the culture medium enters the filter (TFF-101) and the biomass is retained within the lumen, due to the filter cut-off.
- the material is either recirculated to the production tank by using the PS-122 stream or continues to further downstream processing. If necessary, the circulation direction can be reversed (creating a countercurrent) to eliminate obstruction due to material built up in the filter, which is generally observed in the initial portion of the filter.
- the filter flow can also be inverted from a luminal to transluminal direction (or from a transluminal to luminal direction) to favor the dislodging of retained material. The pumps and valves involved in this flow inversion operations are not shown.
- TV-01 is a three-way valve that can allow the mixing of recirculated product with the material from the production tank resulting in a concentration and/or temperature conditioning prior to entering to TFF-101.
- TFF-101 is a mixed-type filter allowing the filtration of the material but also the diffusion of a particular gas composition into the liquid material.
- the filtrate from TFF-101 is transferred to tank TK-101 for extra filtration in TFF-102 or recirculation by the bypass activated by pump PV-105.
- the TFF-102 ensures the removal of small molecules and ions, retaining proteins and bigger molecular weight products in the biomass extract retained within the TFF-101.
- the recirculation involves the passage through a heat exchanger (THE-101) to adjust the temperature of the recirculating liquid to ensure a proper temperature during heat treatment of the biomass retained at TFF-101.
- TFF-101 heat exchanger
- the filtered supernatant from the first phase of operation (concentration) is directed to storage tanks for subsequent processing, for extra processing, whereas after the first phase of liquid reduction, the liquid is recirculated for temperature and composition control, and RNA derived compound extraction.
- the material is subjected to diafiltration to remove the compound dissolved in the liquid from the biomass or transferred to a separation device for liquid-solid separation to obtain a solid cake.
- Example 1c Application in RNA reduction using a DSM type filter
- FIG. 4 is a schematic diagram of an exemplary system for RNA reduction and biomass processing configuration using a DSM type filter with gas composition control for oxygen control within the filter.
- the biomass suspended in the culture medium enters the filter (DSM-100) and the biomass is concentrated, and oxygen supplied to avoid hypoxia. Then, the concentrated suspension of biomass is directed to HL-100 for steam infusion for heat control and then kept at RNA degradation temperature for RNA reduction within the holding tank HT-100. Then, it is transferred to the TK-108 where further heat treatment if required takes place.
- the filtrated from DSM-100 is directed to tank TK-107 and filtered by the filter TFF-102 for recirculation in the filter or liquid recycling in the process. Once heat treatment is completed the material is subjected to final solid liquid separation to obtain the biomass and the biomass extract ready to be dried or used as is
- Perfusion in a continuous bioreactor with biomass (total or partial) retention using filtering sleeves or tangential flow filtration apparatuses is affected by the CO 2 built up and O 2 reduction in the filtering device, furthermore, the change in the temperature impacts cell productivity.
- the control of the gas composition and temperature within the filtering devices with gas phase or gas vector control strategies in this invention greatly improves the performance of perfusion cultures outperforming currently available perfusion systems (See Fig. 3 ).
- the filtering device is either a mixed fiber cartridge (for hollow fiber) or a mixed layer cassette, being particular fibers or layers within the device aimed for gas composition and/or temperature controlling function in order to ensure conformation of a filtering device with tight control of the conditions.
- silicone fibers allow the O 2 transfer
- fluorinated polymer fibers are used for heat control applications and regular filtering material fibers for perfusion purposes.
- the arrangement of the fibers and composition can be varied in order to suit the particular requirements of the cell being treated.
- Example 3 Use of a static filter for partial dewatering for heat treatment improvement and recirculation.
- the liquid stream from the bioreactor is separated in a filtering device allowing the retention of most of the solid material and obtaining a filtrate that can be circulated back to the bioreactor for water saving and nutrient recycling.
- the filtrate may or may not be processed depending on the quality in terms of contamination control of the filtering device.
- the filtering device is indicated as DSM-100.
- the material with partial liquid reduction named PS-122 is directed to a heat treatment device by either direct steam injection or heat exchange. The biomass coming from the bioreactor is rejected in the filter, and then concentrated.
- Recirculation of the liquid for multiple times ensures a more efficient filtration as the effective filter cut off size of the filter is reduced due to bed formation from material retained on the filtering surface, increasing the retention capacity expected for the particular screen used (i.e., the filter retains smaller particles and the yield on filtrable solids is increased).
- the condensation of steam results in increased volume and high temperature zones.
- a heat exchanger is preferred, including, but not limited to cask and tube type. As the temperature-controlled processes require a particular residence time, the material is kept at temperature in piston flow or similar equipment allowing control of reaction or treatment time on the product.
- the extra concentration in the liquid stream resulting from DSM-100 and the proper control of the gas composition within this operation allow for reduction of the energy required for subsequent separation of the compounds derived from heat treatment of the PS-122 stream.
- This sensitive reduction of energy consumption renders recovery of the compounds obtained from this stream possible, changing the economy of processes involving heat treatment for proper conditioning of filtrate materials (for example unicellular protein, filamentous fungi biomass, animal derived products with high RNA content).
- the material stream (PS-124) is directed to further processing, for example solid-liquid separation to obtain liquid-free heat-treated material (i.e. RNA reduced biomass able to be consumed).
Landscapes
- Engineering & Computer Science (AREA)
- Life Sciences & Earth Sciences (AREA)
- Chemical & Material Sciences (AREA)
- Biotechnology (AREA)
- Organic Chemistry (AREA)
- Bioinformatics & Cheminformatics (AREA)
- Health & Medical Sciences (AREA)
- Wood Science & Technology (AREA)
- Zoology (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Biochemistry (AREA)
- Biomedical Technology (AREA)
- General Engineering & Computer Science (AREA)
- General Health & Medical Sciences (AREA)
- Genetics & Genomics (AREA)
- Sustainable Development (AREA)
- Microbiology (AREA)
- Apparatus Associated With Microorganisms And Enzymes (AREA)
- Preparation Of Compounds By Using Micro-Organisms (AREA)
- Micro-Organisms Or Cultivation Processes Thereof (AREA)
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US202163282083P | 2021-11-22 | 2021-11-22 |
Publications (1)
Publication Number | Publication Date |
---|---|
EP4183864A1 true EP4183864A1 (fr) | 2023-05-24 |
Family
ID=84361136
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP22208948.4A Pending EP4183864A1 (fr) | 2021-11-22 | 2022-11-22 | Procédé et dispositifs pour une séparation solide-liquide partielle ou totale efficace à l'aide de conditions contrôlées par gaz |
Country Status (2)
Country | Link |
---|---|
US (1) | US20230159882A1 (fr) |
EP (1) | EP4183864A1 (fr) |
Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2008245537A (ja) * | 2007-03-29 | 2008-10-16 | Toray Ind Inc | 連続発酵による化学品の製造方法 |
EP2837687A1 (fr) * | 2012-03-30 | 2015-02-18 | Toray Industries, Inc. | Procédé de fabrication d'un produit chimique au moyen d'une fermentation continue et dispositif de fermentation continue |
US20160102287A1 (en) * | 2011-12-14 | 2016-04-14 | Kiverdi, Inc. | Method and Apparatus for Growing Microbial Cultures that Require Gaseous Electron Donors, Electron Acceptors, Carbon Sources, or Other Nutrients |
WO2018002581A1 (fr) | 2016-06-27 | 2018-01-04 | Marlow Foods Limited | Champignon comestible |
WO2018002579A1 (fr) | 2016-06-27 | 2018-01-04 | Marlow Foods Limited | Procédé de réduction du taux d'arn dans une biomasse comprenant des champignons filamenteux |
US20210079334A1 (en) * | 2018-01-30 | 2021-03-18 | Genomatica, Inc. | Fermentation systems and methods with substantially uniform volumetric uptake rate of a reactive gaseous component |
-
2022
- 2022-11-22 US US17/992,343 patent/US20230159882A1/en active Pending
- 2022-11-22 EP EP22208948.4A patent/EP4183864A1/fr active Pending
Patent Citations (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2008245537A (ja) * | 2007-03-29 | 2008-10-16 | Toray Ind Inc | 連続発酵による化学品の製造方法 |
US20160102287A1 (en) * | 2011-12-14 | 2016-04-14 | Kiverdi, Inc. | Method and Apparatus for Growing Microbial Cultures that Require Gaseous Electron Donors, Electron Acceptors, Carbon Sources, or Other Nutrients |
EP2837687A1 (fr) * | 2012-03-30 | 2015-02-18 | Toray Industries, Inc. | Procédé de fabrication d'un produit chimique au moyen d'une fermentation continue et dispositif de fermentation continue |
WO2018002581A1 (fr) | 2016-06-27 | 2018-01-04 | Marlow Foods Limited | Champignon comestible |
WO2018002579A1 (fr) | 2016-06-27 | 2018-01-04 | Marlow Foods Limited | Procédé de réduction du taux d'arn dans une biomasse comprenant des champignons filamenteux |
GB2551964A (en) | 2016-06-27 | 2018-01-10 | Marlow Foods Ltd | Edible fungus |
GB2557886A (en) | 2016-06-27 | 2018-07-04 | Marlow Foods Ltd | Edible fungus |
US20210079334A1 (en) * | 2018-01-30 | 2021-03-18 | Genomatica, Inc. | Fermentation systems and methods with substantially uniform volumetric uptake rate of a reactive gaseous component |
Also Published As
Publication number | Publication date |
---|---|
US20230159882A1 (en) | 2023-05-25 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
Giorno et al. | Biocatalytic membrane reactors: applications and perspectives | |
Nunez et al. | Cell immobilization: Application to alcohol production | |
US8679778B2 (en) | Method for producing a biopolymer (e.g. polypeptide) in a continuous fermentation process | |
EP2252699B1 (fr) | Production de galacto-oligosaccharides par Bullera singularis et Saccharomyces sp. | |
Fuchs et al. | Scale-up of dialysis fermentation for high cell density cultivation of Escherichia coli | |
Chang et al. | Multi-stage continuous high cell density culture systems: a review | |
US4764471A (en) | Continuous bioreactor and process | |
Lewandowska et al. | Ethanol production from lactose in a fermentation/pervaporation system | |
Buque-Taboada et al. | In situ product recovery (ISPR) by crystallization: basic principles, design, and potential applications in whole-cell biocatalysis | |
Mattiasson et al. | Extractive bioconversions with emphasis on solvent production | |
Chang | Membrane bioreactors: engineering aspects | |
Chang et al. | Cell retention culture with an internal filter module: continuous ethanol fermentation | |
JPH0595778A (ja) | 撹拌機を装備した多孔質分離膜一体型培養器 | |
EP4183864A1 (fr) | Procédé et dispositifs pour une séparation solide-liquide partielle ou totale efficace à l'aide de conditions contrôlées par gaz | |
Ryu et al. | Comparative study of ethanol production by an immobilized yeast in a tubular reactor and in a multistage reactor | |
JPS61249396A (ja) | イソマルツロ−スの酵素による連続式製造法 | |
Mehaia et al. | Membrane bioreactors: Enzyme processes | |
Märkl et al. | A new dialysis fermentor for the production of high concentrations of extracellular enzymes | |
Paterson et al. | Sorbitol and gluconate production in a hollow fibre membrane reactor by immobilized Zymomonas mobilis | |
HÄggström et al. | Continuous production of butanol with immobilized cells of Clostridium acetobutylicum | |
WO2004046351A1 (fr) | Controle de reactions de biocatalyse | |
CN110938138B (zh) | 一种同时提取藻蓝蛋白和甘油葡萄糖苷的方法 | |
Taillandier et al. | Deacidification of grape musts by Schizosaccharomyces entrapped in alginate beads: a continuous-fluidized-bed process | |
DK144277B (da) | Femgangsmaade til fremstilling af 6-aminopenicillansyre | |
KR20090027217A (ko) | 효모 발효 음료의 제조 방법 |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
PUAI | Public reference made under article 153(3) epc to a published international application that has entered the european phase |
Free format text: ORIGINAL CODE: 0009012 |
|
STAA | Information on the status of an ep patent application or granted ep patent |
Free format text: STATUS: THE APPLICATION HAS BEEN PUBLISHED |
|
AK | Designated contracting states |
Kind code of ref document: A1 Designated state(s): AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC ME MK MT NL NO PL PT RO RS SE SI SK SM TR |
|
STAA | Information on the status of an ep patent application or granted ep patent |
Free format text: STATUS: REQUEST FOR EXAMINATION WAS MADE |
|
17P | Request for examination filed |
Effective date: 20231124 |
|
RBV | Designated contracting states (corrected) |
Designated state(s): AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC ME MK MT NL NO PL PT RO RS SE SI SK SM TR |